Production of paraffins



Dec. 2, 1947. M. P. MATUszAK PRODUCTION oF PARAFFINS Filed Dec. 27, 1945 INVENTOR. MP. MATuszAK ATTORNEYS Patented Dec. 2, 1947 PRODUCTION F PARAFFINS Maryan P. Matuszak, Bartlesville, Okla., assignox' to Phillips Petroleum Company, a corporation of Delaware Application December 27, 1945, Serial No. 637,383

1.3 Claimsl This invention relates to a process for reacting parailins and olens in the presence of a liquid acid-type catalyst to produce other paraiiins. More specifically, in one modification, it relates to the production of especially desirable paraiiins diierent in molecular structure from the products resulting from simple unctures of the original parains and olefns. This application is a continuation-impart of my copending application Serial No. 467,872, filed December 4, 1942, now Patent 2,399,368, granted April 30, 1946, which in turn is a continuation-impart of my application Serial No. 404,395, led July 28, 1941.

In present-day acid-catalyzed alkylation processes for reacting parains with oleflns to produce heavier parains, the principal or major constitu ents of the alkylates produced under ordinary good reaction conditions are those which would be formed if one oleiin molecule added to one paran molecule by a reaction generally termed parailin-olen juncture. At least in some cases, apparently a methyl group from the original Vparaiin becomes attached to one of the two double-'bond carbon atoms of the original olen and the rest of the original parafn becomes attached to the other double-bond carbon atom of the original olein, In any event the number of carbon atoms per molecule of the major chemical components of the product is equal to the sum of the numbers of carbon atoms per molecule of the paraiin and olen reactants. Further, only a `limited number of the many parain isomers characterized by this number of carbon atoms per molecule are form-ed as primary products of simple parailn-olen junctures, although other isomers may be formed in small proportions by so-called secondary and side reactions, such as isomerization of the primary product, .dimerization of the original olen accompanied or follogved by hydrogenation of the dimer, and the 1l e.

vThose skilled in `the Vart of alkylationhave hitherto directed their efEQrts Amainly towards ,increasing the extent of the simple paraffin-olefin Ijuncture and towards decreasing the extent of side reactions, especially polymerization of the' olen. However, in many instances, speccside reactions other than polymerization ,producecon- 2 paraiiin with the initial olen. Further, these specific desirable side reactions may be greatly and selectively promoted yin accordance with the concept of the present invention.

One obect of my invention is to react hydrocarbons to produce other hydrocarbons.

An object of this invention is to produce paraff ns by an alkylation process wherein certain desirable side reactions, which ordinarily occur to only a limited extent, are selectively promoted so that they occur to a much larger extent.

Another lobject of this invention is so to react isobutane .and an olefin other than isobutylene and having three to five carbon atoms per molecule as to obtain high yields of 2,2,4-trimethylpentane (isooctane).

A further object of my invention is to produce parailin hydrocarbons.

Another object of this invention is to produce isooctane, which has eight carbon atoms per molecule, from isobutane and propylene, which have four and three carbon atoms per molecule, res pectively,

Another object -of this invention is Tto increase the proportion of 2,2,4etrimethylpentane pro.- duced ,by reacting isobutane and butene-Z in the presence of a liquid acid-type alkylation catalyst. Another object of this invention is to increase the proportions of 2,2,4-trimethylpentane and 2,3,4-trimethylpentane produced by reacting isobutane and butene-l in the presence of a liquid acid-type alkylation catalyst.

Another obect oi this inventionis to increase the total yield of higher boiling and normally liquid or gasoline-range paraiims .produced from a given Weight of an olenic reactant in acidcatalyzed conversion of isopentane to heavier parans.

Another object of 4this invention is to produce high proportions of isobutane and isohexanes from isopentane and an olen in the presence of a liquid acid-type alkylation catalyst.

Other objects 4and advantages ,of this invention will appear from the accompanying description and discussion.

This invention, in a 'broad sense, comprises pro.- ducing from parans and olens in the presence of a liquid acid-type alkylation catalyst desirable saturated hydrocarbons 4 having molecular struclitres different from thpsacf the products `0f Simple primary junctures of the original parailins and oleflns. In a more limited sense, it comprises selectively producing specific parafllns which are normally not present or at most present in only relatively small proportions in the products from acid-catalyzed alkylations of the original parafns with the original olefins. In other words, it comprises selectively promoting specific side reactions, other than polymerization of oleflns, in acid-catalyzed alkylation of parafns with oleiins.

One particularly noteworthy side reaction selectively promoted in accordance with the present invention results in the over-al1 effect of a hydrogen-transfer from the reactant paraflin to the olenic reactant, followed by juncture of the resulting dehydrogenated paraffin or newly formed olen with unreacted paraffin. This reaction produces a by-product paraffin having the same number of carbon atoms per molecule as the olenic reactant, and a product paraffin having exactly twice as many carbon atoms per molecule as the original parain in the feed. This reaction is particularly desirable when isobutane is being reacted with propylene, normal butenes, or amylenes, especially when a plentiful supply of isobutane is available, since the product contains large amounts of 2,2,4-trimethylp`entane (isooctane), which is desirable because of its high octane rating.

Isobutane and propylene ordinarily yield 2,3- and 2,4-dimethylpentanes by simple parainolefin juncture, Whereas they yield propane and octanes (mostly isooctane) by the hydrogen transfer-alkylation herein described. Isooctane has a higher octane rating (A. S. T. M. octane No.=100) than these dimethylpentanes (A. S. T. M. octane No.=82 and 89 respectively), and the theoretical yield of isooctane based on the weight of propylene in the feed is 2'71 per cent, which is considerably more than the theoretical yield of dimethylpentanes of only 238 per cent. The byproduct propane may be advantageously dehydrogenated in a dehydrogenation step to produce propylene and hydrogen, and the resulting propylene may be returned to the hydrogen-transfer alkylation step.

Although the detailed mechanisms of all the reactions are not yet fully known, the following illustrative chemical equations (2 to 5, inclusive), deduced from data obtained by extensive experimentation, appear to account for some of the principal reactions of isobutane and propylene that can occur under the conditions herein disclosed, as contrasted with the conventional reaction (Equation 1).

Simple paran-olefin juncture (conventional) CiHa CHm CsH (isobutylcne) (isobutane) (isooctaietl obtained from different butylenes.

Isobutane and normal butenes yield 2,3,4-trlmethylpentane and 2,4-dimethylhexane by simple paraffin-olefin juncture, whereas they yield isooctane (2,2,4-trimethylpentane) by the process of this invention. Of these products, isooctane has the highest octane number and is therefore the most desirable for use in such motor fuels as aviation gasoline. Although the hydrogen transfer-alkylation is more desirable, in reacting isobutane and normal butenes, than simple or primary paraiin-olen junctures, another overa1l reaction, which may be called olen isomerization-alkylation" and which normally occurs to only a relatively minor extent, is even more desirable since it avoids the formation of by-product normal butane. This reaction is selectively encouraged in some ways by conditions similar to those which encourage hydrogen transfer-alkylation; it will be discussed hereinafter.

The simple junctures of isobutane with amylencs yield nonanes, which have not yet been positively identified as to particular isomers. The reaction of this invention yields isooctane (2,2,4-tri.. methylpentane) as a product and pentanes as a byproduct. This reaction occurs to an appreciable but minor extent under ordinary alkylating conditions, but by application of the principles of this invention it may be selectively greatly encouraged. The isooctane thus produced as a major product has a higher A. S. T. M. octane number than that of a nonane fraction normally produced (e. g., 91.6). Although the theoretical yield of octanes based on the weight of olefin in the feed by this hydrogen transferalkylation is slightly less than the theoretical yield of nonanes by ordinary alkylation, the byproduct pentanes are also useful for blending in gasoline and should be included in a, consideration of the relative yields. Accordingly, the total theoretical yield of gasoline products (octanes plus pentanes) is 266 weight per cent for the hydrogen transfer-alkylation, or considerably more than that of 183 for the ordinary or simplejuncture alkylation.

Other examples of hydrogen transfer-alkylations are: isobutane and cycloolens to give octanes and by-product cycloparains; isobutane and ethylene to give octanes and ethane; and the like. The reaction of isobutane and cyclooleflns, such as cyclohexene, proceeds readily under about the same conditions as the reaction of isobutane and normal butenes. When ethylene is used, it is desirable to use a relatively high reaction tem perature such as about 20G-406 F., or a very active catalyst to obtain reasonably rapid reaction rates. One of the most satisfactory catalysts for usewith ethylene consists of a mixture of substantially anhydrous hydrofluoric acid having a minor proportion, such as 1 to 10 per cent by weight, of boron fluoride; the small proportion of boron fluoride has a strong promoting or enhancing effect on the catalytic action of the hydrouoric acid.

In the alkylation of isobutane with butylenes, in accordance with one modification of my invention, the over-all reaction already mentioned which may be termed olen isomerization-alkylation tends to minimize differences in products That is, there is a tendency for any given butylene to isomerize, under alkylating conditions, to an equilibrium mixture of the various butylenes. If an equilibrium mixture (thermodynamic equilibrium) were actually obtained before any of the butylenes entered into the alkylation reaction, identical products would be obtained from each of the different lbutylenes. By the application of the present invention, the isomerization of normal butylenes prior to juncture with isobutane can be encouraged to the extent that butene-l gives a product which is similar to that hitherto normally obtained from butene-2, and butene-Z gives a, product which approaches that hitherto ordinarily obtained only from sobutylene.

Another desirable side reaction, which may be selectively encouraged in accordance with the principles of this invention, occurs normally only to a minor extent in the alkylation of isopentane with olefins. This side reaction results in an apparent disproportionation of isopentane to isobutane and isohexanes (2- and 3-methylpentanes). For example, under some conditions, which are especially effective in the alkylation of isopentane with olens in the presence of anhydrous hydrofluoric acid, a surprisingly large proportion of the isopentane is converted to isobutane and isohexanes, concurrently with primary alkylation of another part of it, so that yields of hexanes and higher-boiling gasoline hydrocarbons as high as 500 or more per cent by weight of the olen in the feed are obtained. This disproportionation-alkylation may be advantageously carried out in a combination alkylationfractionation equipment wherefroin isobutane is distilled overhead, in company with some hydroiiuoric acid, while the reactions are progressing. The isobutane produced by the disproportionation may be used as feed stock for other processes, as for a process in which it itself is alkylated; in the interest of an increased yield of higher-boiling or gasoline hydrocarbons from the disproportionation-alkylation, the isobutane is preferably removed from the reaction mixture as soon as possible after formation, and it is preferably not recycled with unreacted isopentane te this particular process.

In addition to being based in part on the observation that in many alkylations using a liquid acid-type catalyst, especially hydrouorio acid, certain side reactions lead to products which in specific instances are more desirable than the primary or simple paraffin-olefin juncture products, the present invention in some of its features involves the following general principles:

1. Different reactions have different temperature coeilcients of reaction rates, so that certain reactions may be selectively encouraged by selecting and controlling the temperature and the reaction time.

2. Over-all or mass reaction rates are dependent upon concentrations of reactants, so that certain reactions may be selectively encouraged by suitably controlling concentrations of reactants.

With respect to the first of these principles, in the concept of this invention, an increase in reaction temperature favors hydrogen transferalkylation and disproportionation-alkylation, and disfavors olefin isomerization-allrylation` relative to simple or primary alkylation. That is, increasing the temperature increases the reaction rates of hydrogen transfer and of disproportionation relatively more than the reaction rate of primary alkylation, and it increases the reaction rate of olefin isomerization relatively less than the reaction rate of primary alkylation. The practical temperature range is of course limited by excessive cracking reactons or decompositions at the upper limit and by disadvantageously low reaction rates at the lower limit. Within the practical temperature range, the optimum temperature for favoring the desired side reaction may be readily determined by trial for any particular case. For promoting hydrogen transfer-alkylation and disproportionation-alkylation, a temperature in the upper part of the practical range is to be preferred; for promoting olenisomerizationalky1- ation, a temperature in the lowerv part of the practical range is to be preferred. The practical temperature range varies somewhat with specific catalyst and reactants, but for the sake of concreteness it may be said to be roughly from about -20 F. to about 300 F. for such a catalyst as hydrogen fluoride and for olens other than ethylene. The reaction temperature is interrelated with the reaction time, for the reaction time required to effect a given extent of reaction is generally shorter at a high temperature than at a low temperature.

With respect to the second of these principles, in general, the desired side reactions are preferentially favored if the concentration of free olefin is minimized by reaction with the catalyst before the olefin can react with the paraffin by primary alkylation or with additional olefin by polymerization. Although oleflns readily add to hydrogen fluoride or undergo hydroiiuorination, to form alkyl fluorides, the part played by this reaction in primary paraffin-olefin and olefin-olefin junctures in the presence of concentrated hydrofluoric acidV as a catalyst is that of a reversible side reaction, not that of an intermediate reaction; that is, these primary juncture reactions comprise the addition of an activated paraffin molecule or of an activated olefin molecule directly to a simple olen molecule, and alkyl fiuorides or similar olefin derivatives undergo these reactions only after being converted to simple olefins. Hence, the rates of primary paraflin-olen and olefin-olefin junctures are decreased by lowering of the concentration of free or uncombined olefin in the reaction zone. Conversely, the rates of the competitive side reactions, in which the olefin appears to take part relatively more effectively in the form of a cornpound cr complex with the catalyst, as illustrated by Equations 2 to 5, are simultaneously increased. Specific examples of such side reactions are those involving hydrogen transfers, olefin isomerization, and the like.

As the catalyst, liquid substantially anhydrous hydrofluoric acid is preferred because it is advantageously appreciably soluble in paramn hydrocarbons and withal it is readily removable and/or recoverable from them. The solubility of hydrofluoric acid in paramns is illustrated by the solubility of hydroiiuoric acid in isobutane, which has been experimentally determined to increase with temperature substantially linearly from 0.3 to 0.9 per cent by weight in the temperature range of 32 to 140 F. A concentration of uniformly dispersed hydroiiuoric acid of between about 0.6 and 4 per cent by weight is preferred. However, the invention is generally applicable with minor modifications to mixtures of other liquid acidtype condensation catalysts with a large proportion of hydroiluoric acid, such as sulfuric acid and hydrofluoric acid, er mixtures of hydroiiucric acid with chlorosulfonic acid, fiuorosulfonic acid, phosphoric acid, phosphoric acid-boron fluoride mixtures, aluminum chloride suspended or dissolved in various solvents, hydroiiuoric acid containing small proportions of dissolved substances such as boron fluoride, and the like. Hydrofluoric acid is usually preferred in many alkylations because it results in a more clean-cut reaction and the ranges of operating conditions used with it are generally broader and more readily controllable than with other catalysts. Since higherthan-usual temperatures are generally desirable in the practice of my invention, catalysts which act as oxidizing agents at such temperatures are often not suitable for use in the commercial practice of my invention. When ethylene and/ or normal paraflins are reactants and hydrofluoric acid the catalyst, however, it is desirable to add a small proportion, such as 1 to 10 per cent by weight, of boron fluoride to the hydrofluoric acid to increase the activity of the catalyst.

Although one excellent method of obtaining maximum concentrations of combined olen with minimum concentrations of free olen evidently involves the direct use of alkyl compounds, such as alkyl fluorides, alcohols, and the like, instead of olens, as alkylating agents, in practice this method makes necessary the use of a separate step for producing alkyl compounds from olefins. A simple method not requiring such an extra step is advantageous in commercial applications. In accordance with one aspect of the present invention, results approaching the ideal are obtained by adding the olen as a gas or vapor to an alkylation zone containing a liquid mixture of liquid hydrofluoric acid and liquid hydrocarbons (both alkylatable paraln hydrocarbon and alkylate product) and a substantial vapor space above the liquid mixture. This vapor space should be of a sufficient size, correlated with the size of the reactor and the degree of agitation of the liquid mixture, that it is substantially free from liquid particles. In small reactors the vapor space will have to be at least equal to, and often several times (such as two to iive times) greater than the volume of the liquid mixture, while with larger reactors a volume no more than about one-third to one-half the volume of the liquid mixture will be sucient, provided that the top of the reactor is suiciently high above the average surface of the agitated liquid mixture to contain only a minor amount (such as less than of liquid particles or droplets. By adding the gaseous olefin to this vapor space at a point where it does not contact immediately large quantities of liquid hydrofluoric acid catalyst, and at a rate such that there will always be a molar ratio of vaporous hydrogen fluoride to olefin of at least 1:1, the

formation of catalyst-olefin addition products or .i

complexes is favored without appreciable undesirable consumption of olefin by polymerization, hydropolymerization, conjunct polymerization, and the like. Once formed, these addition products apparently do not react extensively with alkylatable paraflns to produce the ordinary paraiin-olein juncture products until they pass into the liquid mixture and therein are reconverted to olens, either the same as the original olens or different from them, thereby causing a delay in the effecting of paraffin-olefin junctures and consequently presenting opportunities for such desirable side reactions as hydrogen transfers, olen isomerizations, and disproportionations to occur. Under usual conditions there will be at least 10% by volume of hydrogen uoride in the vapor phase. Thus with a liquid mixture of isobutane and hydrouoric acid (each present in amounts such that there vare separate liquid phases) the vapor phase at F. will contain aproximately 28 per cent by volume of hydrogen fluoride.

An understanding of some aspects of this invention may be aided by reference to the drawing, which is a flow-diagram of one preferred arrangement of apparatus suitable for practicing the invention. This diagram obviously cannot show all possible variations and minor modifications of the invention and should not be used to limit the invention unduly. For the sake of concrete illustration but without limiting the invention, the reactants will be assumed to be isobutane and propylene, and the alkylating catalyst will be liquid anhydrous hydrofluoric acid.

Propylene, which is a specific example of an olen other than isobutylene having three to five carbon atoms per molecule, is admitted through inlet I0 into the top part of the vapor zone of reactor I4.

Reactor I4 may be any suitable vessel resistant to corrosion by hydroluoric acid and provided with a mixing device, such as one or more :Iettype and/or perforated plate-type inlets, baflles, or stirrers, such as paddles I2' rotated by motor II, capable of maintaining liquid hydrocarbons and liquid hydrofluoric acid in a state of intimate mixture. Liquid concentrated or substantially anhydrous hydrofluoric acid is introduced to the liquid zone of reactor I4 through conduit 49. The

relative proportions of hydrofluoric acid and hydrocarbon and the conditions of temperature and pressure in reactor I4 should be such that two distinct liquid phases are present in the liquid zone. Usually a volume ratio of hydroiuoric acid to hydrocarbon in the range of 0.3:1 to 2:1 is preferred and the optimum ratio appears to be 1:1, however, volume ratios outside this range may be used, although if they are much higher or lower, good-contacting of acid with hydrocarbon becomes relatively diicult to maintain. The temperature may be in the range of about 0 to 200 F., a temperature above about 100 F. is preferred and is readily obtained because the over-al1 heat elfect from the reactions is exothermic. The pressure will be that of the vapor pressure of the mixture at the reaction temperature.

After a suitable average residence time in reactor I4, for example a time in the range of l to 30 minutes, the liquid reaction mixture passes through conduit IE to settler I1, where it is sep' arated, as by gravitational and/or centrifugal means, into two liquid phases. Most of the denser or liquid hydrofluoric acid phase is recycled through conduit I8 to reactor I4; a small proportion is usually passed through conduit I9 to acid-rerun column 2!! for puriiication before re-use. A part of the lighter or hydrocarbon phase may be recycled through conduit I5 to the liquid zone of reactor I4. The remainder, or all, of this phase is passed through conduit 22 to deisobutanizer 23, wherein it is separated into two fractions, a low-boiling fraction comprising isobutane and propane and minor amounts of hydrofluoric acid, and a high-boiling fraction comprising higher-boiling product paraflins, mostly gasoline-range paraflins. The low-boiling fraction is passed through conduit 24 to depropanizer 25, and the high-boiling fraction is passed through conduit 2B to defluorinator 21, or directly to fractionating means 43 through conduit 5I.

Depropanizer 25, which also includes means for removing hydrofluoric acid, separates propane from isobutane. The propane is passed through conduit 28 to dehydrogenator 29, wherein it is cracked noncatalytically or, preferably, dehydrogenated catalytically to produce propylene. Additional propane may be introduced to dehydrogenator 29 through inlet 3B.

Propylene-containing eluent from dehydrogenator 29 is passed through conduit 3l to column 32, wherein hydrogen, methane, and other materials boiling lower than propylene are separated and are removed therefrom through conduit 33. The propylene may be concentrated by being ractionally distilled and then may be used as olefinic feed, but it is preferably passed together with the propane directly through conduit 34 to conduit l0 as the olenic feed. The propane acts as a desirable inert material in the reaction zone. Although, in ordinary alkylations, inerts are usually considered undesirable because of adverse effects upon equipment capacities, the presence of inert materials is somewhat advantageous in the present process by selectively promoting desirable reactions such as hydrogen-transfer reactions. Apparently the advantage results from a decrease in the rate of primary paraffin-olefin junctures, owing to a lowering of the isoparaiiin concentration in the reaction zone, thus increasing the proportion of olefin undergoing hydrogen transfer prior to addition to the isoparailn. Similarly, the presence of inerts promotes isomerizations of 1oleiins to 2-oleins and of secondary olefins apparently to isoolens prior to alkylation in systems in which normal butylenes and/or amylenes are used to react with isobutane.

Isobutane from the bottom of depropanizer 25 is passed through conduit 35 directly either to conduit l or to saturator 35, wherein it is agitated and becomes saturated with hydrofluoric acid admitted through conduit 37. Additional isobutane may be introduced through inlet 56, to replace that consumed in the process.

The isobutane-hydrofluoric acid mixture from saturator 35 passes through conduit 38 to settler 3S wherein it is separated, as by gravitational and/or centrifugal means, into two liquid phases. The upper phase, comprising isobutane and a minor proportion of hydroiiuoric acid, is passed through conduit @d to conduit l5, and then to reactor lll. The lower, or hydrofluoric acid phase, is recycled through conduit il to reactor lll.

In deiluorinator 2? the deisobutanized material from deisobutanizer 23 is passed over a Contact material having some degree of catalytic dehydrogenatlon power, such as a supported nickel catalyst, or, more ecomonically, a granular aluminous material such as bauxite or Fullers earth, at a temperature in the range of about 20G-500 F., to remove organically combined fiuorine. The uorine-free product material passes through conduit 42 to fractionating means 43.

Fractionating means 43 may consist of one or more columns suitably designed for separating the total product material into desired fractions, such as a. major gasoline-range fraction, which may be withdrawn through outlet 44, and a minor high-boiling fraction, which may be withdrawn through outlet 5. Substantially pure isooctane may be advantageously separated as a major fraction and may be withdrawn through outlet 4S, instead of being left in the gasoline-range fraction.

Acid column 20 separates used hydroluoric acid into a major overhead fraction of substantially pure or anhydrous hydroluoric acid and a bottom fraction of tar, water, and other impurities which gradually accumulate in the acid during l0 use. The overhead fraction is recycled through conduit 47 to reactor I4 and/or to saturator 36. The impurities are withdrawn through outlet 48. Make-up acid enters the system at some point such as inlet 49.

It will be understood that the flow-diagram is schematic and that auxiliary equipment, not shown or described, such as pumps, valves, controllers, and the like, may be desirable or even necessary at various points in the process. As such auxiliary equipment are well-known, they can be readily supplied by those skilled in the art.

As has already been indicated, otherolelns, such as the butylenes and the amylenes, may be used instead of propylene. However, in practical applications of this invention to the conversion or" low-boiling isoparairins, some choice as to particular olens is somewhat desirable. For example in the alkylation of isobutane with isobutylene, the preliminary hydrouorination step of this invention is of not such noteworthy advantage as it is in the alkylation of isopentane with isobutylene. The reason for this differentiation is that the delay in parainn-olen juncture effected by the preliminary hydrofluorination of isobutylene leads to no discernible advantage when the original isoparain is isobutane, since the nature of the product is not improved, whereas this hydrofluorination leads to increased disproportionation to isobutane and isohexanes when the isoparahn is isopentane. The invention is of most practical benet in the alkylation of isobutane with secondary or normal olens having three to ve carbon atoms per molecule, as both the hydrogen-transfer and the olenisomerization reactions favored by it lead to the production of product parans of advantageously relatively high octane rating. In the alkylation of isopentane, an advantage of the invention is most marked when the olen is butene-l, for upon isomerization of this olefin and upon subsequent juncture of isopentane with the resulting butylene isomer, product paraflins of higher octane rating are obtained than when the olefin in Ythe paraiiln-olen juncture is the original butene-l. Insofar as disproportionation of isopentane to isobutane and isohexanes is concerned, it may be noted that the presence of the added olen in some form or other is advanta- The following examples are illustrative of some of the many aspects of the invention Without necessarily being limitative.

EXAMPLE I selected conditions; that is, the propylene was added as a vapor at one-sixth of the rate used in the rst run, the addition ybeing made at a high and relatively quiescent point in the reactor at which the wall was only wetted by the mixture of isobutane and hydrofluoric acid, so that a considerable part of the propylene formed isopropyl uoride before becoming mixed with the main body of the well-agitated two-liquid-phase mixture of isobutane and hydrouoric acid. The conditions in this second run were thus relatively favorable to the occurrence of hydrogen transfer from isobutane to propylene prior to rapid alkylation, since the propylene came into contact for a relatively long time with only a limited amount of hydrofluoric acid, which was suicient to form isopropyl fluoride but was relatively insulicient to act as a catalyst promoting ordinary alkylation and/or polymerization. The reactions were stopped by stopping the stirring and by letting the reaction mixture separate into two liquid layers when the propylene had been in the reactor for 11.5 to 16.0 minutes in the first run and 7.0 to 25.0 minutes in the second run; thus the calculated average reaction time was about the same in both runs, being 13.8 minutes in the rst and 16.0 minutes in the second. The yields of liquid paraifins were about the same in both runs, but the quantitative proportions of the individual paramns differed greatly, as is shown by the following data:

The product from the run made under selected conditions had more than twice as much isooctane (2,2,4-trimethylpentane) as that from the run made under ordinary conditions, and in consequence it had a considerably higher antiknock rating. The fact that it had a relativeliT somewhat higher content of high-molecular- Weight compounds'should not be construed as a disadvantage, for the run was made under conditions that were exploratory and far from optimum, so that an undesirable amount of polymerization actually occurred because of the presence of some excess liquid hydrofluoric acid during the hydrofluorination of the propylene; under more closely controlled conditions, as when the propylene is added to isobutane containing substantially only a minor proportion of entrained and/or dissolved hydrofluoric acid, such polymerization is Virtually eliminated.

EXAMPLE II In a batch-type run made at 97-105 F. in an 18-liter steel reactor provided with a 540-R. P. M. stirrer, liquid isobutane was thoroughly mixed with about a third of its volume of liquid anhydrous hydrouoric acid, and 0.10 of its molecular equivalent of. isopropyl fluoride, which had been made by reacting propylene and anhydrous hydrofluoric acid, was added at a uniform rate during 13 minutes. The reaction mixture Was stirred for 7 additional minutes, so that the reproduct has an action time was 7 to 20 minutes, or an average of 13.5 minutes. The reaction mixture was then separated into two liquid phases, and the upper or hydrocarbon phase was freed from acid and was fractionally distilled to recover the liquid product. This product amounted to 226.4 per cent by weight of the propylene equivalent of the isopropyl uoride. Its composition in per cent by volume was: hexanes, 3.7; heptanes, 36.6; octanes (mostly isooctane), 55.2; heavier paraffins, 4.5. The aviation-gasoline fraction, cut at 376 F., amounted to 99.7 per cent by volume and had an octane number of 93.4.

EXAMPLE III When butene-l is used instead of propylene in the process of Example II, the gasoline-range A. S. T. M. octane rating about two to three units higher than that of the gasoline-range product obtained by the ordinary alkylation process from the same quantities of materials under substantially the same conditions except that the preliminary hydrofluorination of the olen is omitted. Thus, instead of an octane number of about 89 characteristic of the product obtained by ordinary alkylation of isobutane with butene-l at a temperature of about F. and a contact or reactor-residence time of about 10 minutes, an octane number of about 92 is obtained. This improvement in octane rating illustrates the advantage obtained by the present invention, presumably through hydrogen transfer and/or olen isomerization.

EXAMPLES IV 'ro IX Data for several batch-type runs for the conversion of isopentane in the presence to hydrofluoric acid, using various olens, are presented together, for the sake of brevity and conciseness, in the following tabulation.

In the run with propylene, Example IV, the amount of isobutane formed was not determined, but it was probably approximately molecularly equivalent to the hexanes (isohexanes), which constituted over 30 per cent of the liquid product. This run was made at an insufficiently high temperature for optimum results, but it is clear that a high extent of disproportionation occurred in spite of this fact.

Among other things, it may be noted from these data that the yield of depentanized liquid product was much higher than that to be expected from ordinary alkylation, being as high as over twice the theoretical alkylation yield computed on the basis of one molecule of olen reacting with one molecule of isopentane. Yields even higher than those shown are obtained at relatively higher temperatures, such as temperatures in the preferred range of 1D0-200 F. With respect to the two runs made with isobutylene, the yield was highest in the run that was made at the relatively higher temperature. Temperatures below about 40 F. are relatively disadvantageous. In al1 these runs, more than one molecule of isopentane reacted per molecule of olen to give higher-boiling parafns; indeed, in the highertemperature run with isobutylene over ve molecules of isopentane reacted per molecule of olen. Since olens, because of their relatively greater readiness to react chemically, are in general more valuable than the corresponding paraiiins, a maior advantage of the disproportionationalkylation here exemplied is obvious.

Dzsproportzonatzon-alici/lation of zsopentane Example IV V VI VII VIII IX Olffl11 .v 05H10 Temperature, F.. 86 73-100 Reaction time, min -70 10-30 10-30 10-30 10-30 9-31 Isopeutane/olen (Mol.) (feed) 7. 25 8. 75 7. 62 8.31 7. 5 10. 2 Hydrocarbons/HF (vol.) 7. 6 1 1 1 1 l Isobutane formed, Wt. per cent of olefin 261 200 155 187 165 Peutane-free liquid product Yield:

Wt. per cent of olefin 406 535 443 405 445 437 Wt. per cent of Theoretical alkylation yield 136 234 194 177 195 216 Composition, vol. per cent:

Hexanes 30. 7 45. 2 42. 3 37. 7 41. 4 49. 5 Heptanes. 8.8 10.2 9.0 5. 1 6. 7 7. 5 Octanes 41. 7 5. 8 11. 6 6. 4 7. 7 3.4 11g onanes 2g. 22. g 37. 0 32. 2 21. 9 ecanes. l0. 15. 4 Hemer-- 3. 4 2. o 4. 3 13 8 12 0{ 2. s

Total. l00- 0 100. 0 100. 0 100. O 100.0 100.0

Aviation-gasoline fraction:

Cut point, F 338 289 289 284 293 29.3 Yield, vol. per cent. 95.1 81. 4 76.2 80.7 34.3 78. 0 Reid vapor pressure, lb 3. 2 4. 65 4. 60 4.45 4. 10 5. l5 Gravity, A. P. I 71. 2 75. 6 75. 2 74. 6 73. 7 76. 4 A. S. T. M. distillation, F.-

First drop 133 143 143 142 145 140 10% eVap 173 153 155 155 16]. 150 evap. 213 175 177 183 191 166 90% evap 274 264 273 271 268 284 End point 344 334 328 321 336 332 A, S. T. M. octane no.:

0 cc. TEL 7.5 0 75.0 76. 2 74. 6 79. 2 72. 2 l cc. TEL 88. 7 90.1 87.7 89.3 86.3 Total Products, Wt. 796 643 560 632 602 Another maJOl advantage 1S DIOVlded by the 30 it should be observed that the reactions proexceedingly high yield of eoncomitantly formed isobutane, which was of the order of twice the original olefin by Weight. This isobutane is of particular value because present sources of this hydrocarbon are inadequate to meet the demand for isobutane as a feed for the manufacture of high-octane aviation gasoline by alkylation. Therefore, this concomitantly formed isobutane may be advantageously separated, preferably as soon as possible after formation, and it may be alkylated with an olefin to aviation-gasoline paraflins in a, separate alkylation unit, preferably in the presence of hydrofluoric acid as catalyst. This procedure is relatively more advantageous than recycling the isobutane together with unreacted isopentane back to the first or isopentanealkylation unit, for the over-all yield of gasolinerange liquid parains for the two-stage operation is considerably larger than for the one-stage operation. Furthermore, the liquid product from the. alkylation of isobutane is considerably higher in octane rating than the liquid product from the disproportionation alkylation of isopentane with the same olefin; for example, the aviation-gasoline alkylate from hydrofluoric acid alkylation of isobutane With isobutylene has an octane number of about 95-96, Which is 2O units higher than the values given in the foregoing tabulation for the aviation-range fraction of the product from the conversion of isopentane. Hence, because of the present demand for high-octane aviation gasoline, the two-stage operation yielding two gasoline-range vproducts is relatively more advantageous than the one-stage operation having combined recycling of isobutane and unreacted isopentane. However, this one-stage operation is not outside the broadest scope of this invention.

The isohexanes produced by the disproportionation may be similarly advantageously separated from the product, as by fractional distillation, and may be used as such for blending in motor fuels or may be alkylated with an olefin, as in the presence of hydrofluoric acid, to give paraflins of dierent volatility.

edge.

moted in accordance With this invention do not comprise secondary reactions such as for example that of cracking subsequent to ordinary alkylation. In such cracking-alkylation, the reactant isoparafn is alkylated with an olefin as in ordinary alkylation and the resulting alkylate is allowed to crack into smaller compounds. Obviously, such cracking-alkylation results in little or no improvement in the over-all yield of paraflins heavier than the original paraffin, Whereas by the present invention the over-al1 yield of such heavier parailins is markedly increased, and to a surprisingly and quite unexpectedly high degree in the light of past knowlfollowing alkylation, the present process promotes reactions preceding or accompanying alkylation.

In accordance With this invention, certain desirable reactions are selectively promoted that ordinarily occur to only relatively minor extents in alkylations of parafns With olens in the presence of liquid acid-type alkylation catalysts. Because the invention may be practiced otherwise than as specifically described or illustrated, and because many modifications and variations Within the spirit and scope of it will be obvious to those skilled in the art of hydrocarbon conversion, the invention should not be unduly restricted by the foregoing specification and examples.

I claim:

l. A process for producing octanes from propylene and isobutane, which comprises intimately admixing in a reaction zone, comprising a liquid Zone and a vapor zone, a liquid mixture comprising isobutane and hydrofluoric acid While at a reaction temperature and pressure and with a volume ratio of hydrofluoric acid to hydrocarbon in the range of 0.3:1 to 2:1, adding to said vapor zone of said reaction zone propylene vapor at a rate such that said propylene reacts with hydroluoric acid present therein to yield isopropyl fluoride prior to becoming mixed with said liquid mixture, and recovering from said liquid mixture Briefly, instead of promoting reactions l a hydrocarbon fraction comprising octanes so produced.

2. A process for converting a low-boiling ncrmal olefin and a low-boiling isoparafn into at least two different parafns, one corresponding to said normal olefin and one having twice the number of carbon atoms per molecule as said isoparaiim, which comprises intimately admixing in a reaction zone, comprising a liquid zone and a vapor zone, a liquid mixture comprising a lowboiling isoparaiin and hydrofluoric acid while at a reaction temperature and pressure and with a volume ratio of hydrofiuoric acid to hydrocarbon in the range of 0.3:1 to 2:1, adding to said vapor zone of said reaction zone a low-boiling normal olefin as a vapor at a rate such that said oleiin reacts with hydroiiuoric -acid present therein to yield the corresponding alkyl iiuoride prior to becoming mixed with said liquid mixture, and recovering from said liquid mixture a hydrocarbon fraction comprising a paraffin hydrocarbon having twice the number of carbon atoms per molecule as said low-boiling isopara'in.

3. A process for the production of normally liquid paraiiin hydrocarbons from lower-boiling isoparains such as isobutane and isopentane, which comprises intimately admixing in a reaction zone, comprising a liquid zone and a vapor zone, a liquid mixture comprising such a lowboiling isoparaiiin and a hydrofluoric acid catalyst while at a reaction temperature and a pressure substantially that of the vapor pressure of said mixture, continuously adding to said vapor zone of said reaction zone a low-boiling olefin as a vapor at a rate such that said oleiin reacts with hydrofluoric acid present therein to yield the corresponding alkyl uoride prior to becoming mixed with said liquid mixture, continuously adding as liquids to said liquid zone additional amounts of said low-boiling isoparain and of hydrofluoric acid, continuously removing from said reaction zone a portion of said liquid mixture and recovering therefrom higher-boiling normally liquid paraiiln hydrocarbons so produced.

4. The process of claim 3 wherein said lowboilin-g oleiin is a normal olefin.

5. The process of claim 3 wherein said lowboiling olefin has at least one fewer carbon atoms per molecule than said low-boiling isoparalln.

6. The process of claim 3 wherein said reaction temperature is between about 100 and about 400 F. and the ratio of liquid hydroiiuoric acid to liquid hydrocarbons in the reaction zone is in the range of 0.321 to 2:1.

7. A process for the production of normally liquid paraiiin hydrocarbons from isobutane and propylene, which comprises intimately admixing in a reaction zone, comprising a liquid zone and a vapor zone, a liquid mixture comprising isobutane and a hydrofluoric acid catalyst while at a reaction temperature between about 100 and about 300 F. and a pressure substantially that of the vapor pressure of said mixture with a ratio of liquid hydroiiuoric acid to liquid hydrocarbons in the reaction zone in the range of 0.3:1 to

16. 2:1, continuously adding to said vapor zone propylene as a vapor at a rate such that said propylene reacts with hydrofluorio acid present therein to yield propyl fluoride prior to becoming mixed with said liquid mixture, continuously adding as liquids to said liquid zone additional amounts of isobutane and of concentrated hydroiiuoric acid catalyst, continuously removing from said reaction zone a portion of said liquid mixture and recovering therefrom higher boiling normally liquid paraffin hydrocarbons so produced.

8. The process of claim 3 wherein said olefin is propylene.

9. The process of claim 3 wherein said oleiin is a normal butylene.

10. The process of claim 3 wherein said olefin is butene-l.

11. A process for the production of normally liquid paraffin hydrocarbons from a lower-boiling isoparaiin such as isobutane and isopentane and a lower boiling olen, which comprises conducting said reaction in a reaction zone comprising a liquid zone and a vapor zone, maintaining in said liquid zone an intimate admixture of liquid hydrogen fluoride catalyst and liquid isoparain reactant together with paraffin hydrocarbon reaction products while at a reaction temperature and a pressure substantially that of the vapor pressure of said mixture, maintaining in said vapor zone at least 10 per cent by volume of vaporous hydrogen iiuoride and the content of liquid droplets not greater than 10 per cent, continuously adding to said vapor zone said lower-boiling oleiin in gaseous phase at a point where it does not contact immediately large quantities of liquid hydroiiuoric acid catalyst and at a rate such that there is always a molar excess of vaporous hydrogen uoride, continuously adding liquid reactant isoparaiiin and liquid hydrogen fluoride to said liquid zone, continuously removing from said liquid zone a portion of said liquid mixture and recovering therefrom higher-boiling normally liquid parairin hydrocarbons so produced.

12. The process of claim 11 wherein said lowboiling oleiin is a normal oleiin having at least one fewer carbon atoms per molecule than said low-boiling isoparain.

13. The process of claim 12 wherein said olen is propylene.

MARYAN P. MATUSZAK.

REFERENCES CITED The following references are of record in the tile of this patent:

UNITED STATES PATENTS Number Name Date 2,399,368 Matuszak Apr. 30, 1946 2,399,353 Jones Apr. 30, 1946 2,307,799 Linn Jan. 12, 1943 2,342,677 Linn Feb. 29, 1944 2,384,735y Frey Sept. 11, 1945 2.384,736 Frey Sept, 11, 1945 2,387,162 Matuszak Oct. 16,1945 

